WO2010018609A2 - Procédé pour la purification-l'adoucissement de gaz naturel au moyen d'une dissociation contrôlée d'hydrates et de leur utilisation comme séparateurs - Google Patents

Procédé pour la purification-l'adoucissement de gaz naturel au moyen d'une dissociation contrôlée d'hydrates et de leur utilisation comme séparateurs Download PDF

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Publication number
WO2010018609A2
WO2010018609A2 PCT/IT2009/000376 IT2009000376W WO2010018609A2 WO 2010018609 A2 WO2010018609 A2 WO 2010018609A2 IT 2009000376 W IT2009000376 W IT 2009000376W WO 2010018609 A2 WO2010018609 A2 WO 2010018609A2
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Prior art keywords
hydrates
gas
formation
dissociation
process according
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PCT/IT2009/000376
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English (en)
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WO2010018609A3 (fr
Inventor
Carlo Giavarini
Filippo Maccioni
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Universita' Degli Studi Di Roma "La Sapienza"
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Application filed by Universita' Degli Studi Di Roma "La Sapienza" filed Critical Universita' Degli Studi Di Roma "La Sapienza"
Priority to US13/058,807 priority Critical patent/US20110179714A1/en
Priority to EP09741007A priority patent/EP2323751A2/fr
Priority to EA201170329A priority patent/EA201170329A1/ru
Priority to CA2732942A priority patent/CA2732942A1/fr
Publication of WO2010018609A2 publication Critical patent/WO2010018609A2/fr
Publication of WO2010018609A3 publication Critical patent/WO2010018609A3/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/52—Hydrogen sulfide
    • B01D53/526—Mixtures of hydrogen sulfide and carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/108—Production of gas hydrates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/06—Polluted air
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/20—Capture or disposal of greenhouse gases of methane
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present invention concerns a process for purifying-sweetening natural gas by means of controlled dissociation of hydrates (clathrates) and the use of such hydrates as separators. More specifically, the invention concerns a process for separating and/or removing sour gases, such as carbon dioxide and hydrogen sulfide, from natural gas or from the associated gas in petroleum reservoirs, through the formation of mixed hydrates, wherein the selective separation takes place both during the hydrates decomposition, under pressure conditions close to atmospheric pressure and temperatures little below zero, and, thereafter, under pressures and temperatures close to equilibrium values.
  • Natural gas and gas associated with oil reservoirs have become, in the latest years, a strategic energy reserve alternative to conventional energy sources, such as coal and crude oil.
  • Natural gas coming from production sites essentially consists of methane, but also contains higher hydrocarbons (from C 2 to C 5+ ), and, in addition, variable percentages of inert or polluting gases (such as carbon dioxide and hydrogen sulfide) and water. These components, that are normally found in the gaseous phase, must be reduced or removed in order to comply with the pipeline specifications. Such specifications indicate, as concerns hydrogen sulfide (also known as sulfurated hydrogen), a concentration close to zero. On the other hand, the latest discoveries of natural gas reservoirs increasingly evidence the presence of remarkable amounts of hydrogen sulfide and carbon dioxide together with methane.
  • gas hydrates are solid crystalline compounds that form when water combines with small molecules (generally gases), normally at temperatures close to zero and high pressures.
  • Molecules that may form hydrates include not only hydrocarbons such ad methane, ethane and propane, but also carbon dioxide, hydrogen sulfide and nitrogen.
  • water crystallizes in a clathrate structure i.e., as an inclusion complex where small size molecules (former) are trapped in a cage-like lattice structure formed by hydrogen bonded molecules.
  • Hnatov et al. (US Patent US 5434330 to M. A. Hnatov and J. Happel) describe a method purifying natural gas from nitrogen, carbon dioxide and hydrogen sulfide through the formation of gas hydrates with a pre- cooled aqueous solution of methanol. Coming into contact with said solution, the natural gas forms hydrates, thus separating from the polluting gases (which increase in concentration in the gaseous stream), and is then recovered from the hydrates suspension by thermal dissociation.
  • the pollutant is mainly hydrogen sulfide; further, it is to be noted that the use of methanol introduces some complexity in the process and may give rise to environmental concerns.
  • the international patent application publ. No. WO2006/ 002781 discloses a further method for purifying natural gases by means of hydrates.
  • thermodynamic conditions suitable only to the formation of hydrogen sulfide hydrates are used, the latter being separated by sedimentation.
  • the document further teaches to operate on the hydrogen sulfide hydrates by a thermal dissociation, and to recycle the resulting aqueous solution in the same natural gas field or in suitable geological structures.
  • the technological proposal disclosed does not take into account the phenomenon of hydrates formation promotion that the hydrogen sulfide and carbon dioxide hydrates exert on the formation of clathrates of natural gas light components.
  • the cited document only considers the thermodynamics of the process and does not consider that in a gaseous mixture the hydrates formation occurs between water and all the "former" molecules present in the mixture.
  • gases such as hfeS and CO 2 promote the formation of mixed hydrates of natural gas at lower pressures and higher temperatures than the pressures and temperatures typical of each gas individually taken (Sun C. Y., Chen G. J., Lin W. and Guo T. M.; "Hydrate formation conditions of sour natural gases", J. Chem. Eng. Data, 2003, 48, 600-602). Therefore, when carrying out a process such as that dis- closed in WO2006/002781 a partial separation of gas would be obtained, but such separation would not be such as to justify a process effective on an industrial scale.
  • the controlled dissociation of hydrates under low pressures ad pro- posed according the invention is based on a purification process of a natural gas containing significant concentrations of carbon dioxide and hydrogen sulfide. These sour gases tend to favor the hydrates formation, which may be effected at temperatures and pressures much less severe than those characterizing pure methane. According to the invention, it has been found that once a solid solution of mixed hydrates has been obtained, it is possible to obtain a separation by acting only on the operating pressure or on the operating temperature.
  • Such separation procedure may also be applied in the case that the well head is plugged; it is possible to act on the "plug" formed, by mildly disso- ciating the mixed hydrate, thus obtaining a first separation upstream of the first classical separation processes.
  • the present invention specifically provides a process for purifying-sweetening natural gas through the controlled dissociation of the corresponding hydrates, which process comprises, in a sequence, the follow- ing steps: a) forming hydrates of a natural gas, having concentrations of H 2 S and CO 2 of from 10 ppm to 40% by volume, in a reactor and with the addition of water, if not already present in the feedstock, to obtain a first separation step during the formation of the said hydrates; b) downloading from said reactor and separating the gas remaining from step a) which did not form hydrates; c) purifying the hydrates formed in the previous steps by dissociation of the H 2 S hydrates under pressure conditions above 0.1 MPa and at temperatures comprised between O 0 C and -5 0 C 1 to obtain a second separation step during the dissociation of the said hydrates formed in step a); d) downloading the gas produced by the controlled dissociation of step c), enriched in H 2 S; e) obtaining fast dis
  • the claimed process also comprises, further to said step e), the following step: f) recovering the reaction water and recycling it for another sequence of the procedure of hydrates formation from natural gas.
  • step a) of hydrates formation is carried out in a batch reactor in the presence of water or with water in the feedstock.
  • the procedure proposed according to the invention may also be advantageously applied by carrying out, before the operating steps referred to before, a preliminary procedure of "reformation-concentration" of the methane hydrates in the solid phase (which will be described in more detail with refer- ence to the operating Examples) by carrying out a thermodynamic cycle close to the equilibrium curve, with venting of the unreacted sour gas downstream the said "reformation-concentration" procedure, comprising, after the steps a) and b), the following steps:
  • A. f orming hydrates of a natural gas, having concentrations of H 2 S and CO 2 of from 10 ppm to 40% by volume, in a reactor containing therein an already formed hydrate, under pressures and temperatures close to the equilibrium pressure and temperature, to obtain a methane- enriched mixed hydrate and, possibly, light hydrocarbons, and a remaining gas consisting of H 2 S and CO 2 ;
  • B. downloading from said reactor, and separating, the remaining gas from step A) which did not form hydrates, consisting of H 2 S and CO 2 ; the remainder of the process being analogous to steps c) and following as defined above.
  • the said steps A) and B) are cyclically repeated two or more times.
  • conditioning agents suitable to favour the hydrates formation are preferably mixed in the process reaction water, said agents being selected from the group consisting of quaternary ammonium salts, phosphonium salts, mixtures of clayey aggregates containing kaolin and montmorillonite.
  • coformer agents suitable to favour the hydrates formation process, may be added in the reaction water.
  • the said agents may be, for exam- pie, tetrahydrofurane (THF), cyclopentane or mixtures thereof.
  • reaction water may be added in the reaction water, these compounds being preferably selected from the group consisting of glycols and alcohols.
  • Another optional technological solution, finally, is that of employing, two or more reactors working in parallel, in order to assure the continuity of the process.
  • the latent heats during the fast dissociation of the purified hydrates are exploited to obtain a heath exchange in the course of the process.
  • Figure 1 shows the dissociation rate (in % mol/sec) of hydrogen sul- fide hydrates (H2S), of carbon dioxide hydrates (CO2) and methane hydrates (CH4) at 0.2 MPa in the experimental conditions of the second part of the process according to the invention described in Example 1 ;
  • Figure 2 is a diagram taken from the known literature, showing the "self-preservation" effect in the dissociation of methane hydrates at atmospheric pressure and temperatures little below 0 0 C;
  • Figure 3 is a diagram taken from the most recent literature, showing the "reformation-concentration” cycle of methane hydrates, at temperatures little above 0 0 C close to the equilibrium curve on the P-T plane;
  • Figure 4 is a diagram taken from the same literature, showing the experimental behavior of the "reformation-concentration" cycle of methane hydrates;
  • Figure 5 is a simplified block diagram of the process according to the invention, in the embodiment described in Example 2; and Figure 6 is a simplified block diagram of the process according to another embodiment of the invention, as described in Example 3.
  • the contact between water and gas produces 18.4 t of hydrate.
  • the hydrate formed has a mixed composition containing higher percentages of sour compounds (CO 2 , H 2 S), which are formed in less severe thermodynamic conditions, and lower concentrations, with respect to the sour compounds, of methane and other higher hydrocarbons (first separation). Practically, the transformation of the sour components (H 2 S and CO 2 ) from gaseous to solid (hydrate) is complete, with a yield close to 100%.
  • the remaining gas which did not form hydrates substantially consists of light hydrocarbons (methane and ethane in this case), and is extracted from the reaction chamber and sent to storage or to the use thereof.
  • the hydrate present in the reactor, containing methane, carbon dioxide and hydrogen sulfide, is depressurized to 0.1-0.2 MPa and kept at a temperature from -1°C to -2°C. In these conditions, the decomposition rate of hydrates containing hydrogen sulfide and carbon dioxide is about three times the decomposition rate of hydrates containing methane or other light hydro- carbons.
  • the final separation of H 2 S and CO 2 thus, occurs at this stage (second separation stage during the dissociation).
  • the reaction occurs in bulk in a batch reactor.
  • the reactor is repressurized (1-2) and then it is heated up to close to the equili- brium curve (2-3).
  • Tr reactor temperature
  • the equilibrium curve is followed, and then the cycle (1-2-3-1) is repeated.
  • the remaining gas mainly consists of methane, which is extracted from the reaction chamber for being used (second block); - 8000 Nm 3 of the feed mixture are fed to the reaction chamber, thus reaching 9.5 MPa (third block);
  • the reaction chamber is repressurized with the feed gas mixture, reaching the pressure of 9.5 MPa and the temperature of 20 0 C (sixth block); - by heating again to a temperature close to the equilibrium curve and by applying the thermodynamic cycle previously described (3rd d formation /seventh block) a mixed hydrate is obtained having a composition of 88% methane hydrates and 12% hydrogen sulfide hydrates;
  • the remaining hydrate (88% methane and 12% H 2 S) is depressurized to 0.1-0.3 MPa and kept at a temperature between -1 °C and -2°C to allow for the dissociation of H 2 S hydrates (ninth block); in these conditions, the dissociation rate of hydrates containing hydrogen sulfide is about three times the dissociation rate of methane hydrates: the final separation of hydrogen sulfide thus takes place at this stage;
  • Example 2 Taking into account the composition of the gaseous mixture of Example 2 it is possible to separate the sour fraction by operating a part of the process under constant pressure.
  • thermodynamic cycle is reduced to a point, located close to the equilibrium conditions.
  • the process is thus rendered simpler, as shown in Figure 6 of the enclosed drawings.
  • the remaining gas mainly consists of methane, which is extracted from the reaction chamber to be used (second block);
  • the remaining hydrate (88% methane and 12% H 2 S) is depressurized to 0.1-0.3 MPa and kept at a temperature between -1 0 C and -2°C to allow for the dissociation of H 2 S hydrates (sixth block); in these conditions, the dissociation rate of hydrates containing hydrogen sulfide is about three times the dissociation rate of methane hydrates: the final separation of hydrogen sulfide thus takes place at this stage;

Abstract

L'invention porte sur un procédé pour la réduction et/ou l'élimination de gaz corrosifs, tels que le dioxyde de carbone et le sulfure d'hydrogène, à partir de gaz naturel ou à partir de gaz associé à des réservoirs de pétrole, au moyen de la formation d'hydrates mixtes, une séparation sélective étant effectuée à la fois au cours de la décomposition des hydrates, dans des conditions de pression proches de la pression atmosphérique et à des températures un peu au-dessous de zéro et, de préférence, au cours d'une étape préliminaire, avec des pressions et des températures proches des valeurs d'équilibre.
PCT/IT2009/000376 2008-08-14 2009-08-10 Procédé pour la purification-l'adoucissement de gaz naturel au moyen d'une dissociation contrôlée d'hydrates et de leur utilisation comme séparateurs WO2010018609A2 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US13/058,807 US20110179714A1 (en) 2008-08-14 2009-08-10 Process for the purification-sweetening of natural gas by means of controlled dissociation of hydrates and use thereof as separators
EP09741007A EP2323751A2 (fr) 2008-08-14 2009-08-10 Procédé pour la purification-l'adoucissement de gaz naturel au moyen d'une dissociation contrôlée d'hydrates et de leur utilisation comme séparateurs
EA201170329A EA201170329A1 (ru) 2008-08-14 2009-08-10 Способ очистки-обессеривания природного газа посредством контролируемой диссоциации гидратов и их применение в качестве сепараторов
CA2732942A CA2732942A1 (fr) 2008-08-14 2009-08-10 Procede pour la purification-l'adoucissement de gaz naturel au moyen d'une dissociation controlee d'hydrates et de leur utilisation comme separateurs

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITRM2008A000462A IT1391172B1 (it) 2008-08-14 2008-08-14 Processo per la purificazione-addolcimento del gas naturale tramite dissociazione controllata degli idrati e uso degli stessi come separatori.
ITRM2008A000462 2008-08-14

Publications (2)

Publication Number Publication Date
WO2010018609A2 true WO2010018609A2 (fr) 2010-02-18
WO2010018609A3 WO2010018609A3 (fr) 2010-04-15

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PCT/IT2009/000376 WO2010018609A2 (fr) 2008-08-14 2009-08-10 Procédé pour la purification-l'adoucissement de gaz naturel au moyen d'une dissociation contrôlée d'hydrates et de leur utilisation comme séparateurs

Country Status (6)

Country Link
US (1) US20110179714A1 (fr)
EP (1) EP2323751A2 (fr)
CA (1) CA2732942A1 (fr)
EA (1) EA201170329A1 (fr)
IT (1) IT1391172B1 (fr)
WO (1) WO2010018609A2 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2349538A2 (fr) * 2008-11-05 2011-08-03 Water Generating Systems LLC Formation et dissociation accélérées d'hydrate
CN102199461A (zh) * 2011-04-19 2011-09-28 上海吴淞煤气制气有限公司 一种常压间歇式天然气的改制工艺及改制装置
EP2596849A1 (fr) 2011-11-24 2013-05-29 Shell Internationale Research Maatschappij B.V. Procédé pour l'élimination d'un contaminant gazeux, de préférence du H2S à partir d'un flux de gaz contaminé

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2625159C1 (ru) * 2016-11-22 2017-07-12 Андрей Владиславович Курочкин Установка паровой конверсии сернистого углеводородного газа

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU1599063A1 (ru) * 1988-10-03 1990-10-15 Институт Химии Нефти И Природных Солей Ан Казсср Способ очистки природных и попутных газов от сероводорода
US5434330A (en) * 1993-06-23 1995-07-18 Hnatow; Miguel A. Process and apparatus for separation of constituents of gases using gas hydrates
RU2004120794A (ru) * 2004-07-07 2006-01-10 Институт криосферы Земли Сибирского отделени Российской Академии Наук (RU) Способ и устройство для очистки природного газа
WO2006002781A1 (fr) * 2004-06-25 2006-01-12 Eni S.P.A. Procede pour reduire/supprimer la concentration de sulfure d'hydrogene contenue dans le gaz naturel
US20070106101A1 (en) * 2005-11-07 2007-05-10 Holloman Corporation Removal of Inerts from Natural Gas Using Hydrate Formation
US20080072495A1 (en) * 1999-12-30 2008-03-27 Waycuilis John J Hydrate formation for gas separation or transport

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6596911B2 (en) * 2000-02-22 2003-07-22 Baker Hughes Incorporation Composition and method for inhibition of formation of gas hydrates
GB0120912D0 (en) * 2001-08-29 2001-10-17 Bp Exploration Operating Process
US6946017B2 (en) * 2003-12-04 2005-09-20 Gas Technology Institute Process for separating carbon dioxide and methane
FR2866346B1 (fr) * 2004-02-13 2006-04-14 Inst Francais Du Petrole Procede d'extraction d'un anti-hydrates contenu dans des hydrocarbures condenses
US20050261529A1 (en) * 2004-05-18 2005-11-24 Baker Hughes Incorporated Enhancement modifiers for gas hydrate inhibitors
US7597148B2 (en) * 2005-05-13 2009-10-06 Baker Hughes Incorporated Formation and control of gas hydrates

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU1599063A1 (ru) * 1988-10-03 1990-10-15 Институт Химии Нефти И Природных Солей Ан Казсср Способ очистки природных и попутных газов от сероводорода
US5434330A (en) * 1993-06-23 1995-07-18 Hnatow; Miguel A. Process and apparatus for separation of constituents of gases using gas hydrates
US20080072495A1 (en) * 1999-12-30 2008-03-27 Waycuilis John J Hydrate formation for gas separation or transport
WO2006002781A1 (fr) * 2004-06-25 2006-01-12 Eni S.P.A. Procede pour reduire/supprimer la concentration de sulfure d'hydrogene contenue dans le gaz naturel
RU2004120794A (ru) * 2004-07-07 2006-01-10 Институт криосферы Земли Сибирского отделени Российской Академии Наук (RU) Способ и устройство для очистки природного газа
US20070106101A1 (en) * 2005-11-07 2007-05-10 Holloman Corporation Removal of Inerts from Natural Gas Using Hydrate Formation

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2349538A2 (fr) * 2008-11-05 2011-08-03 Water Generating Systems LLC Formation et dissociation accélérées d'hydrate
EP2349538A4 (fr) * 2008-11-05 2013-03-13 Water Generating Systems LLC Formation et dissociation accélérées d'hydrate
CN102199461A (zh) * 2011-04-19 2011-09-28 上海吴淞煤气制气有限公司 一种常压间歇式天然气的改制工艺及改制装置
EP2596849A1 (fr) 2011-11-24 2013-05-29 Shell Internationale Research Maatschappij B.V. Procédé pour l'élimination d'un contaminant gazeux, de préférence du H2S à partir d'un flux de gaz contaminé

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IT1391172B1 (it) 2011-11-18
US20110179714A1 (en) 2011-07-28
CA2732942A1 (fr) 2010-02-18
WO2010018609A3 (fr) 2010-04-15
ITRM20080462A1 (it) 2010-02-15
EP2323751A2 (fr) 2011-05-25
EA201170329A1 (ru) 2011-08-30

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